US5597539A - Catalytic process - Google Patents

Catalytic process Download PDF

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Publication number
US5597539A
US5597539A US08/436,369 US43636995A US5597539A US 5597539 A US5597539 A US 5597539A US 43636995 A US43636995 A US 43636995A US 5597539 A US5597539 A US 5597539A
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Prior art keywords
liquor
oxidant
scrubber
catalyst
recycle
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US08/436,369
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English (en)
Inventor
Martin E. Fakley
Friedrich H. H. Valentin
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Johnson Matthey PLC
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Imperial Chemical Industries Ltd
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Assigned to IMPERIAL CHEMICAL INDUSTRIES PLC reassignment IMPERIAL CHEMICAL INDUSTRIES PLC ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: FAKLEY, MARTIN EDWARD, VALENTIN, FRIEDRICH HEINRICH HERMANN
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Assigned to JOHNSON MATTHEY PLC reassignment JOHNSON MATTHEY PLC ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: IMPERIAL CHEMICAL INDUSTRIES PLC
Assigned to JOHNSON MATTHEY PLC reassignment JOHNSON MATTHEY PLC ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: IMPERIAL CHEMICAL INDUSTRIES PLC
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/485—Sulfur compounds containing only one sulfur compound other than sulfur oxides or hydrogen sulfide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/68—Halogens or halogen compounds
    • B01D53/70—Organic halogen compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/72—Organic compounds not provided for in groups B01D53/48 - B01D53/70, e.g. hydrocarbons
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/73—After-treatment of removed components
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation

Definitions

  • This invention relates to a catalytic process and in particular to a catalytic process for the removal of odours and/or volatile organic compounds from gas streams.
  • gas streams such as air
  • odoriferous and/or volatile organic compounds may be carcinogenic and/or toxic, and/or discharge into the atmosphere may be unacceptable for other reasons.
  • gas streams include the exhaust gases from operations such as meat processing, eg fat rendering; sewage treatment; foundries; paint spraying and the like.
  • objectionable odoriferous substances that may occur in such gas streams include aliphatic amines and aldehydes; sulphur compounds such as hydrogen sulphide, mercaptans and organic sulphides; phenols, cresols, and xylenols; while volatile organic compounds include a wide range of aliphatic and aromatic compounds such as short chain aldehydes, ketones, alcohols, esters, and halogenated hydrocarbons. It is thus desired to treat the gas stream to remove the aforesaid substances and/or to convert then to a less objectionable material. Oxidation often results in the conversion of such substances to less odorous and/or less volatile compounds or to inorganic end products.
  • the gas streams may be treated to remove those substances, and/or render them less objectionable, by passing the gas stream through a scrubber packing in counter-current flow to an aqueous solution containing an oxidant such as hydrogen peroxide or hypochlorite ions.
  • an oxidant such as hydrogen peroxide or hypochlorite ions.
  • the oxidant effects oxidation of the unwanted components to less objectionable compounds.
  • a suitable metal salt eg a nickel salt, such as nickel sulphate, where the oxidant is hypochlorite or an iron salt where the oxidant is hydrogen peroxide
  • a fixed bed of a metal oxide catalyst is utilised: not only are the problems of corrosion and effluent disposal avoided but also the amount of oxidant required to effect the desired degree of treatment may be decreased, and the intensity of oxidation enhanced.
  • the present invention provides a process for the treatment of a gas stream containing one or more volatile organic and/or odoriferous substances comprising passing said gas stream through a scrubbing packing, feeding an aqueous liquor having an oxidant selected from hydrogen peroxide and hypochlorite ions dissolved therein to the packing whereby said liquor flows through the packing in vapour/liquid contact with said gas stream, whereby said substances are scrubbed from said gas stream into the aqueous liquor, and, after passage through said packing, collecting said aqueous liquor containing said substances in a reservoir, taking part of the liquor from said reservoir as recycle liquor, feeding said recycle liquor, together with a fresh aqueous solution of said oxidant, as the aqueous liquor fed to the packing, and passing at least said part of said recycle liquor through a fixed bed of a metal oxide catalyst for the decomposition of said oxidant before mixing said recycle liquor with the fresh oxidant solution.
  • the invention also provides apparatus for the treatment of a gas stream containing one or more volatile organic and/or odoriferous substances comprising: a scrubbing packing; means to feed said gas stream through said scrubbing packing; means to feed an aqueous liquor having an oxidant dissolved therein to said packing whereby said liquor flows through said packing in vapour/liquid contact with said gas stream; a reservoir to collect said aqueous liquor from said packing; means to extract part of the liquor from said reservoir as recycle liquor; means to add a fresh solution of said oxidant to said recycle liquor to form the aqueous liquor fed to said packing; a fixed bed of catalyst for the decomposition of said oxidant; and means to pass at least part of said recycle liquor through said catalyst bed before addition of the fresh oxidant solution to said recycle liquor.
  • the scrubbing packing is preferably disposed in a vertical column to the upper portion of which the aqueous liquor is fed while the gas to be treated is passed up through the column, so that there is counter-current vapour/liquid contact.
  • a horizontal scrubber may be employed wherein the gas passes transversely through the packing while he liquor flows down the packing under the influence of gravity, so that there is transverse-current vapour/liquid contact.
  • part of the aqueous liquor from the reservoir is taken as recycle liquor and fed to means to distribute the liquor over the packing.
  • Fresh oxidant solution is added to the recycle liquor before it is fed to the distributor.
  • Part of the liquor from the reservoir is removed as an effluent stream, preferably before, in the circulation direction, the addition of the fresh oxidant solution.
  • the effluent steam comprises the overflow from the reservoir.
  • a demister is provided so that, after leaving the packing, the treated gas is largely freed of entrained liquor before discharge or further treatment as may be desired.
  • Control of the process is preferably effected by controlling the rate of addition of fresh oxidant solution so as to achieve a desired concentration of oxidant in the effluent stream.
  • This control may be effected automatically by means of a suitable sensor system: thus where the oxidant is a hypochlorite solution, a redox sensor may be used to control the rate of addition of fresh hypochlorite to give a finite, but limited, chlorine content in the effluent stream.
  • the catalyst is preferably not disposed as a bed essentially filling the reservoir. Rather it is preferred that the catalyst is disposed in a recycle conduit so that only that part of the liquor in the reservoir that is being recycled contacts the catalyst.
  • the reservoir is preferably disposed beneath the packing, and the catalyst bed may be located within the reservoir so that gas evolved as a result of the reaction occurring during passage of the liquor through the catalyst mixes with the gas stream undergoing treatment.
  • the catalyst bed can be separated from the remainder of the reservoir by suitable baffles defining the recycle conduit from the reservoir. Alternatively it may be more convenient in some plants to provide the catalyst bed in a separate vessel in the recycle line to which recycle liquor form the reservoir is fed.
  • a conduit preferably having one or more valves to control the flow therethrough, may be provided as a bypass for the catalyst bed.
  • the catalyst bed is dimensioned such that the contact time of the recycle liquor with the catalyst is 1 to 10 sec.
  • the catalyst bed is preferably disposed such that it is filled, ie flooded, with liquor. It will be appreciated that the catalyst bed may in fact comprise more than one volume containing the catalyst through which the recycle liquor passes. Such volumes of catalyst may be disposed in series or in parallel.
  • the catalyst may be in the form of pellets or granules each containing the catalytically active material, which is preferably oxides of at least one metal selected from copper, iron, manganese, chromium, nickel, and cobalt.
  • the catalyst preferably comprises nickel and/or copper, optionally together with oxides of at least one metal selected from iron, manganese, chromium, aluminium, and metals of Group IIa of the Periodic Table.
  • the oxidant is hydrogen peroxide
  • the catalyst preferably comprises oxides of iron and/or manganese, optionally together with oxides of one or more other metals.
  • the catalyst is preferably in the form of an intimate mixture of the metal oxide on a suitable inert, preferably porous, support.
  • suitable catalysts include those described in the aforementioned EP 211530-A. EP 276044-B, or, particularly, those described in U.S. Pat. No. 5,041,408.
  • the support comprises alumina or a calcium aluminate cement.
  • the active catalyst is believed to be the oxides of nickel (or cobalt) in a higher valency state than in the nickel (II) oxide, NiO.
  • nickel (or cobalt) oxides Such higher oxides are conveniently termed nickel (or cobalt) "peroxides" although the presence of a true peroxide linkage is doubtful.
  • the nickel and/or cobalt "peroxides" are preferably formed in situ by oxidation of nickel or cobalt oxide by the oxidant in the liquor.
  • the catalyst Before activation, ie before oxidation to the "peroxide" state, the catalyst preferably contains 10-70% by weight of nickel and/or cobalt oxide, and preferably nickel oxide forms at least 50% by weight of the combined weights of nickel and cobalt oxides.
  • the catalyst preferably contains 0.2 to 10% by weight of iron oxide (expressed as Fe 2 O 3 ) as this has been found to act as an activity promoter.
  • the scrubbing packing is of any suitable material that is inert to the liquor and preferably has a configuration that affords a good vapour/liquid contact with low resistance to the gas flow through the packing.
  • Such packing are well known in the art.
  • the packing is preferably free from catalyst for the decomposition of the oxidant.
  • the aqueous liquor fed to the packing preferably contains 0.25 to 150 millimoles of oxidant per litre and has a pH in the range 9 to 14 when the oxidant is hypochlorite and a pH of at least 7 where the oxidant is hydrogen peroxide.
  • Alkali may be added as well as oxidant solution to maintain the pH within the desired range.
  • the pH and oxidant concentration of the liquor in the reservoir, or of the effluent stream, or of the recycle stream after passage through the catalyst bed may be monitored and the rate of addition of fresh oxidant and alkali (if any) controlled thereby to maintain the monitored pH and oxidant concentration within desired ranges.
  • the aqueous liquor is preferably fed to the packing at a temperature of 5° to 60° C.
  • the volumetric flow rate of gas through the packing is preferably 100 to 1500 times the volumetric flow rate of the aqueous liquor.
  • the gas stream is preferably fed at such a temperature that the aqueous effluent from the bed has a temperature in the range 5° to 60° C.
  • volatile organic and/or odoriferous compounds that may be treated by this process include sulphur compounds, eg hydrogen sulphide; amines; aldehydes; ketones; aromatics; organo-halogen compounds, and solvents such as alcohols and esters.
  • the process is of particular utility in treating gases containing less than 100 g/m 3 of the volatile organic and/or odoriferous compounds.
  • gas streams that may be treated include waste gases from sewage plants, chemical plants, food processing plants, and animal product processing plants, eg fat rendering plants and tanneries, before those waste gases are discharged to the atmosphere.
  • an effluent steam is taken from the reservoir, preferably before passage through the catalyst bed, eg as an overflow from the reservoir.
  • concentration of oxidant in the effluent stream is at a level low enough to be acceptable for discharge.
  • the gas to be treated is fed via line 1 to the lower portion of a column 2 having a packing 3 affording good vapour/liquid contact.
  • the gas passes up the column 2 through the packing 3 and then through a demister 4 to an outlet line 5.
  • a distributor 6 Located in the upper portion of the column 2, below the demister 4, is a distributor 6 to which an aqueous liquor containing the oxidant is fed via line 7.
  • the liquor thus flows under the action of gravity for the distributor 6 down through the packing 3 where it contacts the gas and scrubs odoriferous or volatile organic substances from the gas.
  • the liquor loaded with those substances is then collected in a sump or reservoir 8 at the lower end of the column.
  • An effluent stream 9 is taken as an overflow from reservoir 8 to maintain the liquor level in the reservoir.
  • Reservoir 8 is provided with a region 10 extending over only a minor proportion of the cross sectional area of the reservoir.
  • a fixed bed 11 of granules of a nickel oxide/cement catalyst is disposed supported on a perforate grid (not shown).
  • An outlet recycle conduit 12 extends from below bed 11 to a recycle pump 13 from whence recycled liquor is fed to the distributor via line 7.
  • the catalyst bed may be provided in a separate vessel disposed in the recycle line before or after pump 13.
  • alkali and oxidant solution After passage of the recycle liquor through the catalyst bed, fresh alkali and oxidant solution is added via lines 14 and 15. Sensors (not shown) are provided to monitor the oxidant concentration and pH in the liquor after passage through the catalyst bed and control means (not shown) responsive to those sensors are provided to vary the rate of feed of alkali and fresh oxidant via lines 14 and 15.
  • the alkali and oxidant solutions can be added as concentrated solutions and water added (via another line, not shown) as a diluent and to control the rate of overflow of the effluent stream 9.
  • the concentration of oxidant remaining in the effluent stream 9 may be decreased further by feeding the effluent stream 9, eg by gravity, through a oxidant decomposition tank 17 having an outlet conduit 18 defining the liquid level in the tank 17.
  • Tank 17 is provided with a vertical baffle 19 extending almost to the bottom of tank 17 thus dividing the tank into two serially connected zones 20, 21.
  • Fixed beds 22, 23 of nickel oxide/cement oxidant decomposition catalyst are disposed in the zones 20, 21 beneath the level of the liquor in those zones so that the effluent from the reservoir 8 flows down through zone 20 and up through zone 21 before discharge.
  • oxidant in the liquor is decomposed and the odoriferous or volatile organic compounds are oxidised.
  • the catalyst bed was positioned in a recycle conduit extending across part of the reservoir and separated from the remainder of the reservoir by a baffle arrangement. Liquor was pumped at a rate of about 90 l/s from the reservoir through the catalyst bed.
  • the bed consisted of 0.2 m 3 of granules of a nickel oxide/cement catalyst of the type described in U.S. Pat. No. 5,041,408 disposed such that the contact time of the liquor passing through the bed was about 2.2 s.
  • the volume of the reservoir was about 11.3 m 3 to that the residence time of the liquor therein was about 2 minutes.
  • An aqueous sodium hydroxide solution was added via line 14 to control the pH at 9.8 and the rate of addition of fresh sodium hypochlorite solution (containing about 140 g/l of sodium hypochlorite) and diluent water (approx 1000 l/h) was controlled to give an overflow effluent containing less than 50 ppm by weight of sodium hypochlorite.
  • the overflow effluent flow rate corresponds to the rate of addition of the diluent water, and sodium hydroxide and fresh sodium hypochlorite solutions.
  • the nickel content of the effluent liquor was less than 1 ppm by weight.
  • the rate of addition of the fresh sodium hypochlorite solution via line 15 was about 10 l/h.
  • the experiment was repeated with the omission of the fixed catalyst bed but with a nickel salt solution being added to the recycled liquor.
  • the rate of addition of the fresh hypochlorite solution was about 20 l/h and the effluent liquor had a nickel content of about 50 ppm by weight.
  • the catalyst was disposed as a fixed bed in the gas space above the reservoir instead of in the recycle line.
  • the liquor from the packing passed through the bed before entering the reservoir.
  • the catalyst bed lost activity as a result of the deposition of oily non-volatile components entrained in the gas stream fed to the tower.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Environmental & Geological Engineering (AREA)
  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Health & Medical Sciences (AREA)
  • Water Supply & Treatment (AREA)
  • Hydrology & Water Resources (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Organic Chemistry (AREA)
  • Catalysts (AREA)
  • Treatment Of Water By Oxidation Or Reduction (AREA)
  • Treating Waste Gases (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)
  • Disinfection, Sterilisation Or Deodorisation Of Air (AREA)
  • Crystals, And After-Treatments Of Crystals (AREA)
US08/436,369 1992-11-18 1993-10-25 Catalytic process Expired - Lifetime US5597539A (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
GB9224201 1992-11-18
GB929224201A GB9224201D0 (en) 1992-11-18 1992-11-18 Catalytic process
PCT/GB1993/002196 WO1994011091A1 (fr) 1992-11-18 1993-10-25 Procede catalytique

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US (1) US5597539A (fr)
EP (1) EP0669850B1 (fr)
JP (1) JP2873254B2 (fr)
KR (1) KR100280275B1 (fr)
AT (1) ATE145348T1 (fr)
AU (1) AU670471B2 (fr)
BG (1) BG99648A (fr)
BR (1) BR9307471A (fr)
CA (1) CA2148449C (fr)
CZ (1) CZ126495A3 (fr)
DE (1) DE69306125T2 (fr)
DK (1) DK0669850T3 (fr)
ES (1) ES2093987T3 (fr)
FI (1) FI952392A (fr)
GB (2) GB9224201D0 (fr)
GR (1) GR3021747T3 (fr)
HU (1) HUT72272A (fr)
IN (1) IN187935B (fr)
MY (1) MY115297A (fr)
NO (1) NO304731B1 (fr)
NZ (1) NZ257164A (fr)
PL (1) PL309040A1 (fr)
RO (1) RO113441B1 (fr)
SK (1) SK63695A3 (fr)
TW (1) TW288987B (fr)
WO (1) WO1994011091A1 (fr)
ZA (1) ZA938065B (fr)

Cited By (12)

* Cited by examiner, † Cited by third party
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USH1948H1 (en) 1998-03-20 2001-03-06 The United States Of America As Represented By The Secretary Of The Navy High-activity catalyst for hydrogen peroxide decomposition
GB2369310A (en) * 2000-09-29 2002-05-29 Fluid Technologies Removal of contaminants from gas stream using acidic scrubber and oxidation
US6409981B1 (en) * 1997-04-25 2002-06-25 Imperial Chemical Industries Plc Process for removing chlorine from gas stream
US20090130047A1 (en) * 2007-11-15 2009-05-21 Weiss Carl S Reduction of airborne malodors using hydrogen peroxide and a catalyst-coated media
US20100024644A1 (en) * 2000-03-03 2010-02-04 Temple Stephen R Method and Apparatus for Use of Reacted Hydrogen Peroxide Compounds in Industrial Process Waters
CN101601962B (zh) * 2009-07-03 2011-12-28 北京帝力伟业科技开发有限公司 废气治理系统和方法
CN107321123A (zh) * 2017-04-06 2017-11-07 浙江奇彩环境科技股份有限公司 一种氯化反应有机废气的处理方法及处理系统
CN107434294A (zh) * 2016-05-25 2017-12-05 曾瑞波 一种废液处理装置以及使用该废液处理装置的空污处理设备
US10525410B2 (en) 2013-01-22 2020-01-07 Stephen R. Temple Methods and equipment for treatment of odorous gas steams
US10881756B2 (en) 2012-06-28 2021-01-05 Stephen R. Temple Methods and equipment for treatment of odorous gas streams from industrial plants
US10898852B2 (en) 2016-08-15 2021-01-26 Stephen R. Temple Processes for removing a nitrogen-based compound from a gas or liquid stream to produce a nitrogen-based product
US11389763B2 (en) 2019-08-28 2022-07-19 Stephen R. Temple Methods for absorbing a targeted compound from a gas stream for subsequent processing or use

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AU3800595A (en) * 1994-10-19 1996-05-15 Joachim Kunze Process, device and catalyst for cleaning used air
DE19630043A1 (de) * 1996-07-25 1998-01-29 Krupp Vdm Gmbh Manganhaltiger Katalysator zur Oxidation von Verunreinigungen in sauren Abwässern
GB9702742D0 (en) * 1997-02-11 1997-04-02 Ici Plc Gas absorption
JP2002045436A (ja) * 2000-08-03 2002-02-12 Noritsu Koki Co Ltd 有害物質の分解処理方法とその装置
AU2000265743A1 (en) * 2000-08-17 2002-02-25 Sakari Savikko Method and apparatus for elimination of odour gases
US8298482B2 (en) 2005-06-10 2012-10-30 S.C. Johnson & Son, Inc. Vapor phase hydrogen peroxide deodorizer
AU2006286159A1 (en) 2005-09-01 2007-03-08 Megair Ltd. Method and apparatus for treating biologically contaminated air
WO2007041831A1 (fr) * 2005-10-07 2007-04-19 Groupe Conseil Procd Inc. Procede de reduction de la teneur en formaldehyde d'un gaz
EP2252171A4 (fr) 2008-02-28 2011-07-06 Megair Ltd Dispositif et procédé de traitement d'air et de désinfection
EP2365865B1 (fr) 2008-12-12 2013-05-29 ThyssenKrupp Uhde GmbH Élimination d'azote ammoniacal, de nitrate d'ammonium et de nitrate d'urée par oxydation avec des solutions contenant de l'hypochlorite à partir d'air évacué dans des installations de production d'ammoniac et d'urée
JP5756307B2 (ja) * 2011-03-14 2015-07-29 株式会社一芯 触媒塔及びこれを用いた湿式脱臭装置
KR20130012886A (ko) 2011-07-26 2013-02-05 현대자동차주식회사 광촉매 반응장치 및 이를 이용한 기상 오염물질 처리방법
CN102772995A (zh) * 2012-07-19 2012-11-14 太仓东能环保设备有限公司 一种有机废气处理装置
CN110339713B (zh) * 2019-08-23 2022-02-08 江西樟树冠京香料有限公司 一种挥发性有机物的处理系统及其处理工艺

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DE2624642A1 (de) * 1976-06-02 1977-12-15 Krupp Ag Huettenwerke Verfahren zum katalytischen entgiften von hypochlorithaltigen loesungen
GB2047217A (en) * 1979-04-23 1980-11-26 Osaka Oxygen Ind Process for deodorising waste gas
EP0057624A2 (fr) * 1981-01-19 1982-08-11 Etablissement public dit: CHARBONNAGES DE FRANCE Procédé de désodorisation d'air pollué
DE3221795A1 (de) * 1982-06-09 1983-12-15 Hugo Petersen Gesellschaft für verfahrenstechnischen Anlagenbau mbH & Co KG, 6200 Wiesbaden Verfahren zum kontinuierlichen entfernen von formaldehyd aus einem gasstrom
US4443342A (en) * 1981-03-31 1984-04-17 Interox (Societe Anonyme) Treatment of waste water containing organic sulphur compounds
US4764286A (en) * 1986-06-26 1988-08-16 The Dow Chemical Company Catalytic decomposition of sodium hypochlorite in highly alkaline solutions

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DE2624642A1 (de) * 1976-06-02 1977-12-15 Krupp Ag Huettenwerke Verfahren zum katalytischen entgiften von hypochlorithaltigen loesungen
GB2047217A (en) * 1979-04-23 1980-11-26 Osaka Oxygen Ind Process for deodorising waste gas
EP0057624A2 (fr) * 1981-01-19 1982-08-11 Etablissement public dit: CHARBONNAGES DE FRANCE Procédé de désodorisation d'air pollué
US4443342A (en) * 1981-03-31 1984-04-17 Interox (Societe Anonyme) Treatment of waste water containing organic sulphur compounds
DE3221795A1 (de) * 1982-06-09 1983-12-15 Hugo Petersen Gesellschaft für verfahrenstechnischen Anlagenbau mbH & Co KG, 6200 Wiesbaden Verfahren zum kontinuierlichen entfernen von formaldehyd aus einem gasstrom
US4764286A (en) * 1986-06-26 1988-08-16 The Dow Chemical Company Catalytic decomposition of sodium hypochlorite in highly alkaline solutions

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6409981B1 (en) * 1997-04-25 2002-06-25 Imperial Chemical Industries Plc Process for removing chlorine from gas stream
USH1948H1 (en) 1998-03-20 2001-03-06 The United States Of America As Represented By The Secretary Of The Navy High-activity catalyst for hydrogen peroxide decomposition
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US10881756B2 (en) 2012-06-28 2021-01-05 Stephen R. Temple Methods and equipment for treatment of odorous gas streams from industrial plants
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DE69306125T2 (de) 1997-03-13
DE69306125D1 (de) 1997-01-02
NZ257164A (en) 1996-04-26
RO113441B1 (ro) 1998-07-30
ES2093987T3 (es) 1997-01-01
MY115297A (en) 2003-05-31
JPH07509658A (ja) 1995-10-26
HU9501269D0 (en) 1995-06-28
KR950704023A (ko) 1995-11-17
NO304731B1 (no) 1999-02-08
NO951941D0 (no) 1995-05-16
WO1994011091A1 (fr) 1994-05-26
FI952392A0 (fi) 1995-05-17
CZ126495A3 (en) 1996-01-17
DK0669850T3 (da) 1997-04-28
EP0669850A1 (fr) 1995-09-06
AU5342094A (en) 1994-06-08
BR9307471A (pt) 1999-06-01
SK63695A3 (en) 1996-03-06
HUT72272A (en) 1996-04-29
BG99648A (en) 1996-04-30
CA2148449A1 (fr) 1994-05-26
CA2148449C (fr) 2004-06-22
JP2873254B2 (ja) 1999-03-24
NO951941L (no) 1995-05-16
GB9224201D0 (en) 1993-01-06
GB9321802D0 (en) 1993-12-15
FI952392A (fi) 1995-05-17
ATE145348T1 (de) 1996-12-15
IN187935B (fr) 2002-07-27
AU670471B2 (en) 1996-07-18
EP0669850B1 (fr) 1996-11-20
ZA938065B (en) 1994-05-20
KR100280275B1 (ko) 2001-02-01
PL309040A1 (en) 1995-09-18
GR3021747T3 (en) 1997-02-28
TW288987B (fr) 1996-10-21

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